CN100548424C - Desalination process and device that Msf distillate drives - Google Patents
Desalination process and device that Msf distillate drives Download PDFInfo
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- CN100548424C CN100548424C CNB2005800286949A CN200580028694A CN100548424C CN 100548424 C CN100548424 C CN 100548424C CN B2005800286949 A CNB2005800286949 A CN B2005800286949A CN 200580028694 A CN200580028694 A CN 200580028694A CN 100548424 C CN100548424 C CN 100548424C
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0068—General arrangements, e.g. flowsheets
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
A kind of desalinating process method of producing drinking water may further comprise the steps: extract at least one and distillate logistics (150) from the step (109) of at least one higher temperature of MSF separating technology (100); With described at least one distillate logistics is supplied to the separating technology (200) that moves under the more low temperature lower than described higher temperature at least one step, thereby, and the external heat input of described at least one step or the external heat input of whole technology have been reduced so that maximally utilise the described sensible heat that distillates in the logistics by in described at least one step, carrying out heat transmission.
Description
Technical field
The present invention relates generally to improving one's methods of multistage flash evaporation method (MSF), particularly relate to the multistage flash evaporation way of distillation (MSF distillation) to seawater, produce drinking water thereby promptly seawater is carried out desalination, the present invention also advantageously relates to the certain methods of the MSF way of distillation that comprises the top brine temp (can reach more than 120 ℃ or 120 ℃) that can reach higher.
Background technology
Thereby knownly seawater is carried out desalination produce the conventional method of drinking water and for example comprise multistage flash evaporation method (MSF), multiple-effect distillation (MED), hyperfiltration (RO) and both vapor compression (VC) way of distillation.Above-mentioned each method all is unusual mature technique, has its unique characteristics and restriction separately.Yet above-mentioned each technology all needs independently energy inlet flow.Up to the present, also do not carry out and MSF and MED between, or the relevant research of interaction of the stream of the energy processes between MSF and the RO, also do not propose or the configuration of research related process, thereby so that utilize different operating temperature systems to make that total output reaches maximization under given energy initial conditions.
When seawater distillates when being transferred to a next step in the evaporimeter that logistics under low pressure moves,, the seawater that concentrates carries out the secondary flash distillation in the MSF tube bank thereby distillating the stream portions pressurized.The steam that produces by the distillate flash distillation mixes with the vapor phase that produces by the salt solution flash distillation, therefore can utilize the heat transfer surface of partly having installed, and described part surface can not be used for flash distillation salt solution and concentrate.
Along with the increase of step number, the flow velocity that is collected in the distillate in the distillation tank increases, and the distillation yield of secondary flash distillation also increases thereupon thus.By reducing the effective dose of the distillate that is obtained by the salt solution flash distillation, i.e. secondary flash distillation distillate increases with respect to the ratio of flash distillation salt solution, and this phenomenon has reduced the efficient of step heat transfer mechanisms.
It should be noted in addition: the known layout that is used to collect and transmit the distillation tank from MSF high temperature step to the distillate of low temperature step becomes and becomes increasingly complex, and more and more away from demister and flash distillation salt solution release areas.
" heat radiation " in typical case's MSF equipment thus section utilize outside seawater to cool off maintenance bottom temp step to be in low temperature.
In this radiating segment, the heat transfer surface of having installed both had been used to be used to concentrate the distillate through flash distillation again by concentrating flash distillation salt solution to produce new distillate.Therefore, the efficient of this radiating segment is lower than heat recovery rate in the equipment, and typically, the heat transfer area above 18% is used to concentrate the distillate through the secondary flash distillation.
The multistage flash evaporation distiller is widely used in large-scale desalination project.Their performance depends on spendable maximum brine temp (top brine temp or TBT) and minimum brine temp (bottom brine temp or BBT) in technical process.The difference of TBT and BBT (flash distillation zone) is big more, and the productive rate of equipment is high more.Modern conventional MSF equipment moves under the top brine temp between 105 ℃ to 112 ℃, and the salt solution in the step of the bottom of heat-recovery section and the temperature of distillate change between 65 ℃ to 50 ℃, and depend on the flow velocity and the temperature of refrigerated sea water.A kind of advanced person's MSF equipment combines MSF and makes TBT can surpass 120 ℃ (referring to EP 1206414 (WO 0114256) of Awerbuch) with nanofiltration, this will provide bigger flash distillation scope.The invention of above-mentioned proposition relates to the improvement to the design of MSF equipment, and described improvement allows to be flashed in the radiating segment of evaporimeter from the more salt solution of MSF equipment, and is concentrated in the bigger heat transfer surface that is used for concentrating salt solution.
The result is that the bottom brine temp is lower.
Described invention improves and relies on above-mentioned two kinds of effects to make process yield be improved.
MED The Application of Technology scope relative narrower, and under relatively low temperature, move.The tip designs temperature that is applicable to MED technology changes between 60 ℃ to 70 ℃.
In saturating (SWRO) regeneration technology of seawater reverse osmosis, inverse penetration coefficient and energy consumption depend on feed temperature.Best temperature is in 30 ℃ to 35 ℃ scope, and for standard film, 40 ℃ is technical limiting value.
In the Middle East, winter seawater temperature in 18 ℃ to 28 ℃ scope.At North African Area, winter, the temperature of seawater was lower, reached 14 ℃ to 12 ℃, and from being no more than 28 ℃.The film regeneration rate is defined as the ratio of film infiltration capacity and feedwater flow.Regeneration rate is high more, and the cost of film and operating cost are just low more.Now, be present in limiting factor overslaugh in the Copenhagen water membrane technology reverse osmosis equipment moving surpassing under 39 ℃ the temperature.
Yet best film feed temperature scope is between 28 ℃ to 32 ℃.At low temperatures, the regeneration rate of film is low, and therefore, the hyposmosis amount can be obtained by the film with high energy amount.
Press for a kind ofly,, raise the efficiency and output so that utilize the difference of the operating temperature curve of various types of desalination systems to improve service condition with the advantage of MSF and the advantages technology together of other two kinds of technology MED and SWRO.The present invention utilizes pre-hot sea water RO supply of obtainable sensible heat and/or MED feedwater from the stream that extracts the MSF distillate under high enough temp.
Summary of the invention
The present invention relates to a kind of improved process that seawater is carried out desalination, described process is moved under the process conditions of optimum by MED, RO or other process and MSF are complementary.
The invention provides a kind of be used for producing drink water desalting method, said method comprising the steps of:
A) extract from least one higher temperature level of MSF separating technology at least one and distillate logistics, and
B) with described at least one distillate logistics and be supplied at least one step that under the more low temperature lower, moves in the separating technology than described higher temperature, thereby by in described at least one step, carrying out heat exchange, farthest utilized the described sensible heat that distillates logistics, and reduced outside heat input described at least one step and the overall process process.
According to the present invention, the energy that is associated with distillate that last step from the MSF heat-recovery section extracts can reclaim another power cycle moved under low temperature more or desalination circulation (for example MED or RO).
Especially, thus because the less flash distillation salt solution that can handle large volume of the distillate of radiating segment heat transfer surface load, therefore, extract distillate from the distillate groove of the last step that is arranged in the MSF heat-recovery section and cause the overall performance of MSF to improve.
Preferably, in described at least one step, the supply water of MSF separating technology is subjected to the preheating of described at least one stream.
Desirable is that described at least one step is the step of second separating technology.
Advantageously, the MED of second separating technology under low temperature more, moving, described MED at least in part, is subjected to that described at least one heat that distillates the heat that extracts the logistics drives from MSF.Described at least one distillate logistics and can in a series of flash process process, be flashed, thereby provide heat by salt solution is directly transferred to the MED technical process.
When described second separating process is MED, described at least one distillate logistics and can be flashed with the cooling distillate, and the injected device hot compression of fluid steam reaches a high temperature, and is input to the higher effect group of MED technical process then.
In addition, when described second separating technology is MED, described at least one distillate logistics and can carry out a series of heat exchange steps, in above-mentioned steps, heat is passed to the distillate of MED from distillate stream.
Another kind of optional mode is that second separating technology can be counter-infiltration (RO) process, in this process, from the supply seawater that logistics is used to preheating RO process that distillates of MSF.
Simultaneously, the heat that the form with distillate that extracts from MSF exists can be used as for example energy source of MED technology of low temperature process process.
Particularly, distillate or inject MED with the form of liquid perhaps is flashed and by first step of compression input MED again.
The application of the present invention in the MSF/RO hybrid technique predicted: for example in winter the distillate that extracts is used for heating the seawater that injects RO equipment, can obtains higher RO film regeneration rate.
Directly the result is, can realize a lot of advantages, and described advantage comprises: utilize the energy stream that is produced by the MSF cascade both can realize having more cost-efficient MSF desalination operating procedure, can reduce MED or RO energy consumption of equipment amount again.
Should be noted that: the invention enables to obtain energy from MSF equipment and become possibility, and improved the performance of MSF equipment simultaneously.
Described distillate extraction system from MSF especially also has some other advantage on device/equipment, be actually because distillation tank can be suitable little in the radiating segment and/or can reserve bigger space to demister.Described space is most valuable for the radiating segment that moves under high vacuum, handles the large volume steam, and this will cause producing in the demister high steam flow velocity.
When overflow took place, above-mentioned feature will cause the loss of efficient and high conductivity.At this on the one hand, if thereby to consider to increase obtainable demister space by reducing to distill tank, the performance of MSF can also be further enhanced.From multistage flash evaporation (MSF) step, remove the means that distillate provides increases desalter output.Be included in the step that energy in the distillate depends on place when removing distillate, and described energy can by be flashed in one or more suitable multi-effect distilling process (MED) circulation effect group or another desalination processes of preheating for example the aliment of RO obtain reclaiming.
From last step of the heat-recovery section of radiating segment front, removing under the situation of distillate, in the end the heat of flash distillation is not all useful, necessary or needs for the MSF still-process in step, still can be used to the membrane process process aliment that preheating proposes.
In general, the heat of the distillate of secondary flash distillation is concentrated in heat transfer surface (HTS), and the tubular area that need be used for concentrating, and described zone can be used to concentrate the extra indirect steam by flash distillation salt water generates.Can be used to increase the area of sprayer, particularly in the lower step of MSF by the occupied extra zone of distillate collection channel.
The heat of removing from the MSF step by extracting distillate from MSF can be reached the lower temperature of MED effect group by the secondary flash distillation, thereby the mode preheating aliment of sensible heat by directly contacting both can be provided, also can be by the feed-water heater preheating aliment of MED.
From MSF equipment all or some be arranged on key position step remove the output quantity that distillate will increase the distilled water of existing and MSF equipment in the future.The calorific potential that is included in heat in the distillate and distillate by with MED, the combination of VC or RO technology and obtain reclaiming.To make like this and maximum production not only in MSF, also improve the efficient of other desalinating process simultaneously.Preferred process is to remove distillate every several steps, and available heat is shifted by the mode of carrying out flash distillation in the MED flash tank, this will produce steam and spray the mode preheating aliment of cold aliment with direct contact, perhaps provide steam-steam to feed-water heater.
Description of drawings
Fig. 1 is the schematic flow sheet of integrated hybrid MSF-MED desalinating process process, has used to distillate the direct infusion of logistics as the MED technical process from MSF distillation high temperature step in described technical process.
Fig. 2 is the schematic flow sheet of second kind of hybrid MSF-MED desalinating process process, and in described technical process, distillate is flashed, and steam is injected in the MED technical process.
Fig. 3 is the schematic flow sheet of the third fully-integrated MSF-MED desalinating process process, has utilized in described technical process from the distillate in the MSF technical process, recycle brine and uncondensable gas to improve the performance of MED.
Fig. 4 is the schematic flow sheet of the 4th kind of hybrid MSF-RO desalinating process process, is used to the feedwater from the distillate preheating RO of MSF equipment technical process in described technical process.
Fig. 5 is the curve map of distillate output with respect to the increased percentage of distillate extracted amount.
The specific embodiment
The present invention has improved MSF desalinating process process of the prior art significantly.By reading and understanding feature of the present invention noted earlier and illustrated in the accompanying drawings and principle, the experienced technician of design, production and the desired water desalination system of operation the present invention can put into practice the present invention and recognize its benefit.
According to an aspect of the present invention, its improvement has been to find that the extract of MSF distillate can be used for providing energy to other process cycles of moving under low temperature more.Have been found that also that in addition described extract has brought significantly improving of performance in the MSF desalter, distillate is extracted out from described MSF desalter.It is not disclosed by prior art that these improve raising.
In each embodiment shown in Fig. 1-4, MSF generally is represented as 100, and it comprises heat radiation step 110 and recuperation of heat step 120.
The principle of MSF distillation is fairly simple.It is pressurized and be heated and reach the maximum device temperature that seawater injects (SW).When heated liquid was discharged in the chamber 123, the pressure of wherein said chamber 123 remained in the saturated vapour pressure that is lower than liquid slightly, and a part of flash distillation of water content forms steam.Then, removed the salt solution drop that suspends during by demister at flash-off steam, and be concentrated on the outer surface of transfer pipes.The drop that concentrates enters groove (105) as hot product water.
The salt solution that does not carry out flash distillation enters second Room or step, and flash distillation therein forms steam under low temperature more, has produced the product water of extra quantity thus.Simultaneously, flow to distillate groove in second step from the distillate of first step (101), and discharged a part of heat.Step of step of described flash distillation---process for cooling process repeats, and finally is discharged out equipment with the form of discharging salt solution and product water respectively up to the salt solution of cooling and the distillate of cooling.
The recycle brine stream (121) of the tube interior that concentrates the steam in each step of flowing through is used to remove concentrated latent heat.Like this, recycle brine obtains preheating, has reclaimed the energy of condensing steam simultaneously.In the multistage flash evaporation equipment this part is called as " recuperation of heat " section.Salt solution through preheating finally is elevated to maximum operation temperature in brine heater (122), this brine heater (122) provides steam by external source (S).Be called as the colling end of the equipment of " heat radiation " section, both born the task of removing used heat by the external refrigeration seawater, bearing the task of producing distillate by concentrating part from the flash distillation salt solution of the remainder of heat-recovery section again.The part (111) of the cool stream that goes out from the radiating segment downstream branch is subjected to preheating becomes make-up water.
Particularly, last recuperation of heat step 109 by extracting the MSF evaporimeter of the present invention (alternatively be represented by dotted lines 108) distillate logistics 150, MSF output is improved, and therefore performance also need not to increase any outer flow than significant the reduction not occurring.
In addition, in the device of newly setting up technology, reserved bigger space, thereby allowed equipment performance to be further enhanced to demister.
The energy that distillates logistics is used as the energy source of independent MED separator, and described MED separator represents that with Reference numeral 200 it comprises a series of effect group 201,202,203.
Use distillate to make MED under low-down supply (outside) thermal losses condition, to move, and improved the energy efficiency of system as the thermal source of MED technical process.
It should be noted that: except the raising of performance, the present invention also provides some environmental benefits.As shown in following table 1, by radiating segment, minimum brine temp (BBT) and heat radiation outlet temperature have all reduced with identical seawater velocity.Another kind of optional mode is, can reduce the flow velocity of the cooling water of the radiating segment of flowing through, and perhaps can realize above-mentioned dual mode.Ambient influnence can be improved in above-mentioned two aspects.
Table 1 has been summed up the attainable advantage of the present invention, and the present invention both can reequip the principle at existing position also can introduce new equipment as design data with it.
Table 1: invention summary of benefits tabulation
| Existing equipment (remodeling) | New equipment |
| Under the condition that does not reduce the performance ratio, increased the output quantity of MSF distillate | Increase the output quantity of MSF distillate and increased the equipment performance ratio |
| Extraction can be used for the hot-fluid of another technical process | Extraction can be used for the hot-fluid of another technical process |
| Revise the design arrangement of inner distiller, might increase demister/area of dissipation and reduce the distillate groove | Optimize the design arrangement of inner distiller, might increase demister/area of dissipation and reduce the distillate groove |
| Reduce the speed of demister and increase distillate purity.Thereby keep the main purity that distillates logistics by before radiating segment, removing to handle.Reduce supplementary loss. | Reduce the speed of demister and increase distillate purity.Thereby keep the main purity that distillates logistics by before radiating segment, removing to handle. |
| Reduce the salt solution minimum temperature | Reduce the salt solution minimum temperature |
| Might reduce the consumption of seawater | Might reduce the consumption of seawater |
If the present invention transforms,, will bring inevitable limiting factor because existing design may hinder the zone that increases demister on existing MSF equipment.In this case, as shown in table 1, the output quantity of equipment will increase.The percentage that equipment increases is shown in Fig. 5 and table 2.If the present invention is applied to new MSF equipment, mean that so equally redesign is positioned at the evaporimeter internal placement of last step of radiating segment, providing more space to demister as far as possible, thereby and allow raising performance ratio.
Table 2 shows the comparative analysis result that the MSF equipment to 5MIGD (1,000,000 I.gal/sky) 17 steps carries out, and described equipment moves extracting under the condition that the MSF (according to the present invention) that distillates logistics has same haline water temperature, same ocean temperature, same brine recirculation flow velocity with the 14th step.
Table 2: extracting distillate and do not extracting MSF performance under the situation of distillate
| Parameter | Extract distillate | Do not extract distillate |
| |
110 |
110℃ |
| Minimum brine temp | 41.3℃ | 42.4℃ |
| The distillate flow velocity | 1157.95 ton/hour | 1174.7 ton/hour |
| The performance ratio | 7.46(t/t) | 7.45(t/t) |
| The steam requirement | 155.27 (ton/hour) | 157.74 (ton/hour) |
| Obtainable energy circulates in the downstream | 61384kJ/ |
0 |
The desalter of imagination comprises flash distillation is wanted in discharges from MSF distillate in jar, and cooling off distillate, and the injected device hot compression of flash vapors reaches higher temperature and enters into the higher step of MSF.
An advantage of apparatus of the present invention is to comprise to discharge from MSF wants the distillate of flash distillation in jar, with the cooling distillate, and be concentrated to obtain double distillation output in the technology that distillate and flash vapors are moved under low temperature more, its highest purity is less than .01ppm TDS.
Fig. 1 shows the basic flow sheet of MSF-MED integrated system, and wherein the MED first effect group is to heat by the distillate that extracts from MSF rather than by concentrated steam.
Described MED equipment is all similar with conventional MED equipment in all fields, and its difference only is: the MED first effect group is not supplied with by steam by the distillate that extracts from MSF.By with the fresh seawater in the heat transferred MED effect group, described distillate obtains cooling in the first effect group.
An alternative mode as shown in Figure 2, wherein the MSF distillate is transferred into flash tank, the steam that produces by the distillate flash distillation is reduced to first step of evaporimeter by hot pressing.
The desalter of imagination comprises: thus in the flash tank of a series of generation flash vapors,, distillate and MED carry out heat transmission by directly being contacted.The distillate that will extract from MSF according to desalter of the present invention is transferred in the flash tank so that cool off described distillate, and injected device hot compression reaches higher temperature before flash vapors more efficient group in entering MED simultaneously.
An alternative desalter according to the present invention is provided at the heat transmission of carrying out in a series of heat exchangers between MSF distillate and the MED distillate:
(a) fully-integrated MED-MSF possibility as shown in Figure 3.According to one embodiment of present invention, three that extract from MSF spread and are passed to MED: distillate, and from the uncondensable exhaust outlet and the salt solution outlet of the first effect group.Salt solution is used as the feedwater of MED, and the distillate of heat is used to replace steam.The invention step comprises that extracting MSF salt solution flows to MED technology, this step by transmit salt water extraction to second technology of under low temperature more, moving so that utilize the sensible heat of brine stream, in this case, desalter of the present invention comprises the device that is used to carry out the heat transmission, and this is used to carry out the device of heat transmission for directly contacting to produce a series of flash tanks of flash vapors with MED by salt solution.Interchangeable according to another preferred device comprises from MSF and extracts salt solution, and flash distillation is with the cooling distillate in flash tank, and the injected device hot compression of flash vapors reaches higher temperature to enter more efficient group among the MED.The mode that the another one of apparatus of the present invention is replaced is, this device is provided at the heat transmission of carrying out in a series of heat exchangers between MSF salt solution and the MED aliment.
Under the running temperature of MED equipment, from the MSF step, inject CO
2The risk of magnesium hydrate precipitate will have been avoided producing, thereby advantageously MED equipment can remain under the situation of cleaning.
Operating process as shown in Figure 4 illustrates mixed type MSF/RO equipment, and the RO feedwater of described equipment is by aforementioned MSF distillate heating of extracting.
According to one embodiment of present invention, film injects water and is heated to 28-30 ℃ by the sensible heat of distillate, advantage has been to keep higher film infiltration regeneration rate, lower specific power consumption and kept the more constant operating temperature of film arrival end, thereby the life-span of having improved film.
Desalter according to the present invention provides and has been used to carry out the device that heat is transmitted, and this device that is used to carry out that heat transmits is a series of by the direct flash tank that contacts the generation flash vapors between distillate and the RO aliment.Interchangeable according to another preferred embodiment comprise from MSF, extract will flash distillation in flash tank distillate, and cool off described distillate, the injected device hot compression of flash vapors reaches higher temperature temperature with heating RO aliment.The desalter that another one is replaced is used to conduct the heat exchange between the heat exchanger between MSF distillate and RO aliment.
Curve map shown in Figure 5 is based upon name and has a daily output of above 500 ten thousand I.gals (MIGD).When present output has surpassed 15MIGD, so output quantity will increase in proportion.
Claims (12)
1, a kind of desalinating process method of producing drinking water, described process may further comprise the steps:
A) from the step (109) of at least one higher temperature of MSF separating technology (100), extract at least one and distillate logistics (150); And
B) with described at least one distillate logistics is supplied to the separating technology (200) that moves under the more low temperature lower than described higher temperature at least one step (201), thereby, and the external heat input of described at least one step or the external heat input of whole technology have been reduced so that maximally utilise the described sensible heat that distillates in the logistics by in described at least one step, carrying out heat transmission.
2, desalinating process method as claimed in claim 1, wherein said at least one step are such steps, and in this step, the feedwater of MSF separating technology is subjected to the preheating of described at least one stream.
3, desalinating process method as claimed in claim 1, wherein said at least one step (201) are meant a step in second separating technology (200).
4, desalinating process method as claimed in claim 3, the multi-effect distilling technology (200) of wherein said second separating technology for moving under low temperature more, described multi-effect distilling technology are subjected to driving from the heat that distillates the heat that extracts the logistics from least one of MSF at least in part.
5, desalinating process method as claimed in claim 4, wherein said at least one distillate logistics and in a series of flash process process, be flashed so that provide heat for multi-effect distilling technology by the mode of salt solution by the direct heat transmission.
6, as claim 4 or 5 described desalinating process methods, wherein said at least one distillate logistics and be flashed with the cooling distillate, and the injected device hot compression of fluid steam reaches a high temperature, and is input to then in more efficient group in the multi-effect distilling technology.
7, as claim 4 or 5 described desalinating process methods, wherein said at least one distillate stream carries out a series of heat exchange steps, and in described heat exchange steps, heat has moved on to the multi-effect distilling technology distillate from the distillate circulation.
8, desalinating process method as claimed in claim 3, wherein said second separating technology is a reverse osmosis process, in described reverse osmosis process, is used to seawater that supply with to give reverse osmosis process is carried out preheating from the logistics that distillates of MSF.
9, desalinating process method as claimed in claim 1 wherein is used as the more energy source of low temperature technology with the heat that extracts that the form of distillate exists from MSF.
10, desalinating process method as claimed in claim 9, wherein said more low temperature technology is multi-effect distilling technology.
11, desalinating process method as claimed in claim 10, wherein said distillate is used to supply with multi-effect distilling technology with the form of liquid.
12, desalinating process method as claimed in claim 10, wherein said distillate is flashed, and is compressed and be imported into first step of multi-effect distilling technology again.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB0419117.7 | 2004-08-27 | ||
| GB0419117A GB2417435A (en) | 2004-08-27 | 2004-08-27 | MSF desalination system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101107051A CN101107051A (en) | 2008-01-16 |
| CN100548424C true CN100548424C (en) | 2009-10-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005800286949A Expired - Fee Related CN100548424C (en) | 2004-08-27 | 2005-08-26 | Desalination process and device that Msf distillate drives |
Country Status (12)
| Country | Link |
|---|---|
| EP (1) | EP1781390B1 (en) |
| JP (1) | JP2008510610A (en) |
| KR (1) | KR20070050050A (en) |
| CN (1) | CN100548424C (en) |
| AT (1) | ATE387944T1 (en) |
| CY (1) | CY1107404T1 (en) |
| DE (1) | DE602005005204T2 (en) |
| DK (1) | DK1781390T3 (en) |
| ES (1) | ES2302224T3 (en) |
| GB (1) | GB2417435A (en) |
| PL (1) | PL1781390T3 (en) |
| WO (1) | WO2006021796A1 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7416666B2 (en) | 2002-10-08 | 2008-08-26 | Water Standard Company | Mobile desalination plants and systems, and methods for producing desalinated water |
| KR100781897B1 (en) * | 2006-12-19 | 2007-12-03 | 두산중공업 주식회사 | Hybrid desalination apparatus and method |
| KR100907662B1 (en) * | 2007-09-21 | 2009-07-14 | 두산중공업(주) | MS seawater desalination system equipped with heat pipe heat emitter |
| CN102502902B (en) * | 2011-11-10 | 2013-07-03 | 集美大学 | New multistage flash evaporation seawater desalting system of thermal power plant |
| CN102849887B (en) * | 2012-10-07 | 2013-08-07 | 中国海洋大学 | Seawater desalting method |
| WO2015107250A1 (en) * | 2014-01-20 | 2015-07-23 | Alex Hanganu Research, S.L. | Highly thermally conductive device for multiple-effect water-desalination systems |
| WO2015107249A1 (en) * | 2014-01-20 | 2015-07-23 | Alex Hanganu Research, S.L. | High-efficiency multiple-effect distillation he-med device |
| ES2473190B1 (en) * | 2014-01-20 | 2015-06-11 | Alex Hanganu Research, S.L. | Multi-Effect Distillation Device |
| US10457568B2 (en) | 2014-04-11 | 2019-10-29 | Murdoch University, National Centre Of Excellence In Desalination Australia | Method for desalination |
| CN104089276A (en) * | 2014-06-24 | 2014-10-08 | 首钢京唐钢铁联合有限责任公司 | Multi-stage flash treatment system utilizing exhaust gas and circulating cooling water |
| US10434435B2 (en) | 2016-03-30 | 2019-10-08 | Veolia Water Technologies, Inc. | System and process for preheating evaporator feedwater |
| CN106587233B (en) * | 2016-10-12 | 2019-02-19 | 王文领 | A kind of method of comprehensive utilization of coal chemical industry gasification Heisui River high temperature flashed vapour |
| WO2018132087A1 (en) * | 2017-01-10 | 2018-07-19 | Kuwait Institute For Scientific Research | Combination multi-effect distillation and multi-stage flash evaporation system |
| US11097203B1 (en) | 2020-03-10 | 2021-08-24 | Bechtel Hydrocarbon Technology Solutions, Inc. | Low energy ejector desalination system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1165895A (en) * | 1965-07-15 | 1969-10-01 | Weir Westgarth Ltd | Improvements in or relating to the Desalination of Sea Water and other Saline Waters |
| US3489654A (en) * | 1967-01-09 | 1970-01-13 | American Hydrotherm Corp | Evaporation system and process |
| GB1441463A (en) * | 1972-06-23 | 1976-06-30 | Hitachi Ltd | Multiple effect evaporator |
| JPS5450483A (en) * | 1977-09-30 | 1979-04-20 | Agency Of Ind Science & Technol | Multistage flash evaporator |
| JPS6186989A (en) * | 1984-10-02 | 1986-05-02 | Ishikawajima Harima Heavy Ind Co Ltd | Seawater desalting composite equipment |
| DE3938012A1 (en) * | 1989-11-15 | 1991-05-16 | Serck Como Gmbh | Desalination evaporator for sea-water - comprises initial flash evaporator, external heat exchanger and cleaning system |
| US6508936B1 (en) * | 1997-10-01 | 2003-01-21 | Saline Water Conversion Corporation | Process for desalination of saline water, especially water, having increased product yield and quality |
-
2004
- 2004-08-27 GB GB0419117A patent/GB2417435A/en not_active Withdrawn
-
2005
- 2005-08-26 EP EP05775302A patent/EP1781390B1/en active Active
- 2005-08-26 CN CNB2005800286949A patent/CN100548424C/en not_active Expired - Fee Related
- 2005-08-26 WO PCT/GB2005/003329 patent/WO2006021796A1/en active IP Right Grant
- 2005-08-26 DE DE602005005204T patent/DE602005005204T2/en active Active
- 2005-08-26 DK DK05775302T patent/DK1781390T3/en active
- 2005-08-26 PL PL05775302T patent/PL1781390T3/en unknown
- 2005-08-26 AT AT05775302T patent/ATE387944T1/en active
- 2005-08-26 KR KR1020077004060A patent/KR20070050050A/en not_active Application Discontinuation
- 2005-08-26 JP JP2007528981A patent/JP2008510610A/en active Pending
- 2005-08-26 ES ES05775302T patent/ES2302224T3/en active Active
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Also Published As
| Publication number | Publication date |
|---|---|
| JP2008510610A (en) | 2008-04-10 |
| CN101107051A (en) | 2008-01-16 |
| EP1781390A1 (en) | 2007-05-09 |
| CY1107404T1 (en) | 2012-12-19 |
| GB0419117D0 (en) | 2004-09-29 |
| DE602005005204D1 (en) | 2008-04-17 |
| GB2417435A (en) | 2006-03-01 |
| PL1781390T3 (en) | 2008-08-29 |
| WO2006021796A1 (en) | 2006-03-02 |
| EP1781390B1 (en) | 2008-03-05 |
| DK1781390T3 (en) | 2008-06-30 |
| DE602005005204T2 (en) | 2009-03-12 |
| KR20070050050A (en) | 2007-05-14 |
| ATE387944T1 (en) | 2008-03-15 |
| ES2302224T3 (en) | 2008-07-01 |
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